US10525404B2 - Use of morpholine-based hindered amine compounds for selective removal of hydrogen sulfide - Google Patents
Use of morpholine-based hindered amine compounds for selective removal of hydrogen sulfide Download PDFInfo
- Publication number
- US10525404B2 US10525404B2 US16/095,970 US201716095970A US10525404B2 US 10525404 B2 US10525404 B2 US 10525404B2 US 201716095970 A US201716095970 A US 201716095970A US 10525404 B2 US10525404 B2 US 10525404B2
- Authority
- US
- United States
- Prior art keywords
- acid
- absorbent
- process according
- gas
- fluid stream
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20436—Cyclic amines
- B01D2252/20452—Cyclic amines containing a morpholine-ring
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20478—Alkanolamines
- B01D2252/20489—Alkanolamines with two or more hydroxyl groups
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/304—Hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Definitions
- the present invention relates to amine compounds suitable for removal of acid gases from a fluid stream, especially for selective removal of hydrogen sulfide from a fluid stream.
- the present invention also relates to an absorbent and to the use thereof and to a process for removing acid gases from a fluid stream, especially for selective removal of hydrogen sulfide from a fluid stream.
- Carbon dioxide has to be removed from natural gas because a high concentration of CO 2 reduces the calorific value of the gas. Moreover, CO 2 in conjunction with moisture, can lead to corrosion in pipes and valves.
- Known processes for removing acid gases include scrubbing operations with aqueous absorbent solutions of inorganic or organic bases.
- ions form with the bases.
- the absorbent can be regenerated by decompression to a lower pressure and/or by stripping, whereby the ionic species react in reverse and the acid gases are released and/or stripped out by means of steam. After the regeneration process, the absorbent can be reused.
- a process in which CO 2 and H 2 S, are substantially removed is referred to as “total absorption”.
- removal of CO 2 may be necessary to avoid corrosion problems and provide the required heating value to the consumer, selective H 2 S removal may be necessary or desirable.
- Natural gas pipeline specifications for example, set more stringent limits on the H 2 S level than on the CO 2 since the H 2 S is more toxic and corrosive than CO 2 : common carrier natural gas pipeline specifications typically limit the H 2 S content to 4 ppmv with a more lenient limitation on the CO 2 at 2 vol %.
- Selective H 2 S removal is often desirable to enrich the H 2 S level in the feed to a sulfur recovery, such as a downstream Claus plant.
- Severely sterically hindered secondary amines such as 2-(2-tert-butylaminoethoxy)ethanol (TBAEE), and tertiary amines, such as methyldiethanolamine (MDEA), exhibit kinetic selectivity for H 2 S over CO 2 .
- TAAEE 2-(2-tert-butylaminoethoxy)ethanol
- MDEA methyldiethanolamine
- Such amines are therefore suitable for selective removal of H 2 S from gas mixtures comprising CO 2 and H 2 S.
- These amines do not react directly with CO 2 ; instead, CO 2 is reacted in a slow reaction with the amine and with water to give bicarbonate.
- the reaction kinetics allow H 2 S to react more rapidly with the amine groups of the sorbent to form a hydrosulfide salt in aqueous solution.
- hydroxyl-substituted amines such as those mentioned above has become common since the presence of the hydroxyl groups tends to improve the solubility of the absorbent/acid gas reaction products in the aqueous solvent systems widely used, so facilitating circulation of the solvent through the conventional absorber tower/regeneration tower unit. This preference may, however, present its own problems in certain circumstances.
- a current business driver is to reduce the cost to regenerate and to recompress acid gases prior to sequestration.
- the separation of the acid gases can occur at pressures of about 4,800-15,000 kPaa, more typically from about 7,250-8,250 kPaa.
- the selectivity for H 2 S removal can be expected to decrease markedly both by direct physisorption of the CO 2 in the liquid solvent and by reaction with the hydroxyl groups on the amine compound.
- the CO 2 reacts preferentially with the amino nitrogen, higher pressures force reaction with the oxygens and under the higher pressures, the bicarbonate/hemicarbonate/carbonate reaction product(s) formed by the reaction at the hydroxyl site is stabilized with a progressive loss in H 2 S selectivity with increasing pressure.
- hydroxyl groups tend to impart surfactant properties to the absorbent/acid gas reaction products, thereby potentially causing troublesome foaming phenomena during the operation of the gas treatment unit.
- alkanolamines such as 2-(2-tert-butylaminoethoxy)ethanol may suffer from a marked volatility, causing absorbent losses during the operation of the gas treatment unit.
- US 2015/0027055 A1 describes a process for selectively removing H 2 S from a CO 2 -containing gas mixture by means of an absorbent comprising sterically hindered, terminally etherified alkanolamines. It was found that the terminal etherification of the alkanolamines and the exclusion of water permits a higher H 2 S selectivity.
- WO 2014/001664 discloses compounds of the formula below and their use in the removal of acid gases:
- R 1 through R 4 are selected from H and alkyl, whereas R 5 and R 6 are alkyl or R 5 and R 6 together form a cycle.
- These compounds, incorporating only tertiary amino groups, are expected to exhibit limited H 2 S capacity since H 2 S capacity attributed to tertiary amino groups is known to be lower than that of, e.g., sterically hindered secondary amino groups.
- EP 0 124 835 discloses bis-tertiary amino alkyl derivatives for acid gas removal from gas streams.
- a preferred derivative is bis-(2-morpholino ethyl) ether.
- the compounds constituting the absorbent are to have reduced tendency to foaming and low volatility.
- the absorbents are to have high cyclic capacity.
- the invention further relates to the use of an absorbent for removing acid gases from fluid streams.
- the object is achieved by a process for removing acid gases from a fluid stream, wherein the fluid stream is contacted with an absorbent comprising a solution of a compound of the general formula (I)
- R 1 and R 2 are independently C 1 -C 4 -alkyl
- R 3 is selected from hydrogen and C 1 -C 4 -alkyl
- R 4 , R 5 and R 6 are independently selected from hydrogen and C 1 -C 4 -alkyl
- x and y are integers from 2 to 4 and z is an integer from 1 to 3.
- R 4 , R 5 and R 6 are hydrogen.
- x is 2 or 3.
- y is 2.
- z is 1.
- R 1 and R 2 are methyl and R 3 is hydrogen; or R 1 , R 2 and R 3 are methyl; or R 1 and R 2 are methyl and R 3 is ethyl.
- the compound of the general formula (I) is selected from N-[2-(2-tert-butylaminoethoxy)ethyl]-morpholine and N-[2-(3-tert-butylaminopropoxy)ethyl]-morpholine.
- the compounds of the general formula (I) comprise a secondary amino group and a tertiary amino group.
- the nitrogen atom in the secondary amino group has at least one secondary or tertiary carbon atom directly adjacent.
- the secondary amino group is thus sterically hindered.
- the compounds of the general formula (I) can be prepared in various ways.
- morpholine is reacted with an sec-alkylamino- or tert-alkylaminoalkoxyalkanol such as 2-(2-tert-butylaminoethoxy)ethanol.
- the reaction is suitably effected in the presence of hydrogen in the presence of a hydrogenation/dehydrogenation catalyst, for example of a copper-containing hydrogenation/dehydrogenation catalyst, at 160 to 220° C.:
- an N-((hydroxyalkyl)alkoxy)-morpholine such as N-(2-(2-hydroxyethyl)ethoxy)-morpholine
- a primary amine R 1 R 2 R 3 C—NH 2 can be reacted with a primary amine R 1 R 2 R 3 C—NH 2 .
- the reaction is suitably effected in the presence of hydrogen in the presence of a hydrogenation/dehydrogenation catalyst, for example of a copper-containing hydrogenation/dehydrogenation catalyst, at 160 to 220° C.
- the absorbent used for removal of acid gases from a fluid stream especially for selective removal of hydrogen sulfide from a fluid stream comprising carbon dioxide and hydrogen sulfide, comprises a solution of a compound of the general formula (I).
- the absorbent comprises preferably 10% to 70% by weight, more preferably 15% to 65% by weight and most preferably 20% to 60% by weight of a compound of the general formula (I), based on the weight of the absorbent.
- the absorbent comprises a tertiary amine or severely sterically hindered primary amine and/or severely sterically hindered secondary amine other than the compounds of the general formula (I). Severe steric hindrance is understood to mean a tertiary carbon atom directly adjacent to a primary or secondary nitrogen atom.
- the absorbent comprises the tertiary amine or severely sterically hindered amine other than the compounds of the general formula (I) generally in an amount of 5% to 50% by weight, preferably 10% to 40% by weight and more preferably 20% to 40% by weight, based on the weight of the absorbent.
- the suitable tertiary amines other than the compounds of the general formula (I) especially include:
- Tertiary polyamines for example bis-tertiary diamines such as
- N,N,N′,N′-tetramethylethylenediamine N,N-diethyl-N′,N′-dimethylethylenediamine, N,N,N′,N′-tetraethylethylenediamine, N,N,N′,N′-tetramethyl-1,3-propanediamine (TMPDA), N,N,N′,N′-tetraethyl-1,3-propanediamine (TEPDA), N,N,N′,N′-tetramethyl-1,6-hexanediamine, N,N-dimethyl-N′,N′-diethylethylenediamine (DMDEEDA), 1-dimethylamino-2-dimethylaminoethoxyethane (bis[2-(dimethylamino)ethyl] ether), 1,4-diazabicyclo[2.2.2]octane (TEDA), tetramethyl-1,6-hexanediamine;
- Tertiary alkanolamines i.e. amines having at least one hydroxyalkyl group bonded to the nitrogen atom, are generally preferred. Particular preference is given to methyldiethanolamine (MDEA).
- MDEA methyldiethanolamine
- the suitable severely sterically hindered amines i.e. amines having a tertiary carbon atom directly adjacent to a primary or secondary nitrogen atom
- amines having a tertiary carbon atom directly adjacent to a primary or secondary nitrogen atom especially include:
- 2-(2-tert-butylaminoethoxy)ethanol TAAEE
- 2-(2-tert-butylamino)propoxyethanol 2-(2-tert-amylaminoethoxy)ethanol, 2-(2-(1-methyl-1-ethylpropylamino)ethoxy)ethanol, 2-(tert-butylamino)ethanol, 2-tert-butylamino-1-propanol, 3-tert-butylamino-1-propanol, 3-tert-butylamino-1-butanol, and 3-aza-2,2-dimethylhexane-1,6-diol;
- 2-amino-2-methylpropanol (2-AMP); 2-amino-2-ethylpropanol; and 2-amino-2-propylpropanol;
- Severely sterically hindered secondary alkanolamines are generally preferred. Particular preference is given to 2-(2-tert-butylaminoethoxy)ethanol.
- the absorbent does not comprise any sterically unhindered primary amine or sterically unhindered secondary amine.
- a sterically unhindered primary amine is understood to mean compounds having primary amino groups to which only hydrogen atoms or primary or secondary carbon atoms are bonded.
- a sterically unhindered secondary amine is understood to mean compounds having secondary amino groups to which only hydrogen atoms or primary carbon atoms are bonded.
- Sterically unhindered primary amines or sterically unhindered secondary amines act as strong activators of CO 2 absorption. Their presence in the absorbent can result in loss of the H 2 S selectivity of the absorbent.
- the absorbent is an aqueous solution.
- the aqueous absorbent comprises an acid.
- the absorbent may, as well as water and optionally an acid, comprise one or more water-miscible organic solvents.
- the acid preferably has a pK A of less than 6, especially less than 5, as determined under standard conditions (25° C.). In the case of acids having more than one dissociation stage and accordingly more than one pK A , this requirement is met where one of the pK A values is within the range specified.
- the acid is suitably selected from protic acids (Br ⁇ nsted acids).
- the acid is preferably added in such an amount that the pH of the aqueous solution measured at 120° C. is 7.9 to less than 9.5, preferably 8.0 to less than 8.8, more preferably 8.0 to less than 8.5, most preferably 8.0 to less than 8.2.
- the amount of acid in one embodiment, is 0.1% to 5.0% by weight, preferably 0.2% to 4.5% by weight, more preferably 0.5% to 4.0% by weight and most preferably 1.0% to 2.5% by weight, based on the weight of the absorbent.
- the acid is selected from organic and inorganic acids. Suitable organic acids comprise, for example, phosphonic acids, sulfonic acids, carboxylic acids and amino acids. In particular embodiments, the acid is a polybasic acid.
- Suitable acids are, for example,
- mineral acids such as hydrochloric acid, sulfuric acid, amidosulfuric acid, phosphoric acid, partial esters of phosphoric acid, for example mono- and dialkyl phosphates and mono- and diaryl phosphates such as tridecyl phosphate, dibutyl phosphate, diphenyl phosphate and bis(2-ethylhexyl) phosphate; boric acid;
- carboxylic acids for example saturated aliphatic monocarboxylic acids such as formic acid, acetic acid, propionic acid, butyric acid, isobutyric acid, valeric acid, isovaleric acid, pivalic acid, caproic acid, n-heptanoic acid, caprylic acid, 2-ethylhexanoic acid, pelargonic acid, caproic acid, neodecanoic acid, undecanoic acid, lauric acid, tridecanoic acid, myristic acid, pentadecanoic acid, palmitic acid, margaric acid, stearic acid, isostearic acid, arachic acid, behenic acid; saturated aliphatic polycarboxylic acids such as oxalic acid, malonic acid, succinic acid, glutaric acid, adipic acid, pimelic acid, suberic acid, azelaic acid, sebacic acid, dodecanedioic acid; cycl
- sulfonic acids such as methylsulfonic acid, butylsulfonic acid, 3-hydroxypropylsulfonic acid, sulfoacetic acid, benzenesulfonic acid, p-toluenesulfonic acid, p-xylenesulfonic acid, 4-dodecylbenzenesulfonic acid, 1-naphthalenesulfonic acid, dinonylnaphthalenesulfonic acid and dinonylnaphthalenedisulfonic acid, trifluoromethyl- or nonafluoro-n-butylsulfonic acid, camphorsulfonic acid, 2-(4-(2-hydroxyethyl)-1-piperazinyl)ethanesulfonic acid (HEPES);
- HEPES 2-(4-(2-hydroxyethyl)-1-piperazinyl)ethanesulfonic acid
- organic phosphonic acids for example phosphonic acids of the formula (II) R 9 —PO 3 H (II)
- R 9 is C 1-18 -alkyl optionally substituted by up to four substituents independently selected from carboxyl, carboxamido, hydroxyl and amino.
- alkylphosphonic acids such as methylphosphonic acid, propylphosphonic acid, 2-methylpropylphosphonic acid, t-butylphosphonic acid, n-butylphosphonic acid, 2,3-dimethylbutylphosphonic acid, octylphosphonic acid; hydroxyalkylphosphonic acids such as hydroxymethylphosphonic acid, 1-hydroxyethylphosphonic acid, 2-hydroxyethylphosphonic acid; arylphosphonic acids such as phenylphosphonic acid, tolylphosphonic acid, xylylphosphonic acid, amino-alkylphosphonic acids such as aminomethylphosphonic acid, 1-aminoethylphosphonic acid, 1-dimethylaminoethylphosphonic acid, 2-aminoethylphosphonic acid, 2-(N-methylamino)ethylphosphonic acid, 3-aminopropylphosphonic acid, 2-aminopropylphosphonic acid, 1-aminopropylphosphonic acid, 1-aminopropyl
- R 10 is H or C 1-6 -alkyl
- Q is H, OH or NY 2
- Y is H or CH 2 PO 3 H 2 , such as 1-hydroxyethane-1,1-diphosphonic acid
- Z is C 2-6 -alkylene, cycloalkanediyl, phenylene, or C 2-6 -alkylene interrupted by cycloalkanediyl or phenylene
- Y is CH 2 PO 3 H 2 and m is 0 to 4, such as ethylenediaminetetra(methylenephosphonic acid), diethylenetriamine-penta(methylenephosphonic acid) and bis(hexamethylene)triaminepenta-(methylenephosphonic acid);
- R 11 is C 1-6 -alkyl, C 2-6 -hydroxyalkyl or Y, and Y is CH 2 PO 3 H 2 , such as nitrilotris(methylenephosphonic acid) and 2-hydroxyethyliminobis-(methylenephosphonic acid);
- aminocarboxylic acids having tertiary amino groups or amino groups having at least one secondary or tertiary carbon atom immediately adjacent to the amino group, such as
- ⁇ -amino acids having tertiary amino groups or amino groups having at least one secondary or tertiary carbon atom immediately adjacent to the amino group such as N,N-dimethylglycine (dimethylaminoacetic acid), N,N-diethylglycine, alanine (2-aminopropionic acid), N-methylalanine (2-(methylamino)propionic acid), N,N-dimethylalanine, N-ethylalanine, 2-methylalanine (2-aminoisobutyric acid), leucine (2-amino-4-methylpentan-1-oic acid), N-methylleucine, N,N-dimethylleucine, isoleucine (1-amino-2-methylpentanoic acid), N-methylisoleucine, N,N-dimethylisoleucine, valine (2-aminoisovaleric acid), ⁇ -methylvaline (2-amino-2-methylisovaleric acid), N-
- ⁇ -amino acids having tertiary amino groups or amino groups having at least one secondary or tertiary carbon atom immediately adjacent to the amino group such as 3-dimethylaminopropionic acid, N-methyliminodipropionic acid, N-methylpiperidine-3-carboxylic acid,
- ⁇ -amino acids having tertiary amino groups or amino groups having at least one secondary or tertiary carbon atom immediately adjacent to the amino group, such as 4-dimethylaminobutyric acid,
- aminocarboxylic acids having tertiary amino groups or amino groups having at least one secondary or tertiary carbon atom immediately adjacent to the amino group, such as N-methylpiperidine-4-carboxylic acid.
- inorganic acids preference is given to phosphoric acid and sulfuric acid.
- carboxylic acids preference is given to formic acid, acetic acid, benzoic acid, succinic acid and adipic acid.
- sulfonic acids preference is given to methanesulfonic acid, p-toluenesulfonic acid and 2-(4-(2-hydroxyethyl)-1-piperazinyl)ethanesulfonic acid (HEPES).
- phosphonic acids preference is given to 2-hydroxyphosphonoacetic acid, 2-phosphonobutane-1,2,4-tricarboxylic acid, 1-hydroxyethane-1,1-diphosphonic acid, ethylenediaminetetra(methylenephosphonic acid), diethylenetriaminepenta-(methylenephosphonic acid), bis(hexamethylene)triaminepenta(methylenephosphonic acid) (HDTMP) and nitrilotris(methylenephosphonic acid), among which 1-hydroxyethane-1,1-diphosphonic acid is particularly preferred.
- aminocarboxylic acids having tertiary amino groups or amino groups having at least one secondary or tertiary carbon atom immediately adjacent to the amino group preference is given to N,N-dimethylglycine and N-methylalanine.
- the acid is an inorganic acid.
- the absorbent comprises at least one nonaqueous organic solvent.
- the absorbent contains only a limited amount of water, or essentially no water in addition to the nonaqueous organic solvent. It may be desirable to limit the water content of the absorbent, for example to a maximum of 20% by weight, alternatively to a maximum of 10% by weight, preferably to a maximum of 5% by weight, or a maximum of 2% by weight.
- the nonaqueous solvent is preferably selected from:
- C 4 -C 10 alcohols such as n-butanol, n-pentanol and n-hexanol;
- ketones such as cyclohexanone
- esters such as ethyl acetate and butyl acetate
- lactones such as ⁇ -butyrolactone, ⁇ -valerolactone and ⁇ -caprolactone;
- amides such as tertiary carboxamides, for example N,N-dimethylformamide; or N-formylmorpholine and N-acetylmorpholine;
- lactams such as ⁇ -butyrolactam, ⁇ -valerolactam and ⁇ -caprolactam and N-methyl-2-pyrrolidone (NMP);
- sulfones such as sulfolane
- sulfoxides such as dimethyl sulfoxide (DMSO);
- glycols such as ethylene glycol (EG) and propylene glycol
- polyalkylene glycols such as diethylene glycol (DEG) and triethylene glycol (TEG);
- di- or mono(C 1-4 -alkyl ether) glycols such as ethylene glycol dimethyl ether;
- di- or mono(C 1-4 -alkyl ether) polyalkylene glycols such as diethylene glycol dimethyl ether, dipropylene glycol monomethyl ether and triethylene glycol dimethyl ether;
- cyclic ureas such as N,N-dimethylimidazolidin-2-one and dimethylpropyleneurea (DMPU);
- thioalkanols such as ethylenedithioethanol, thiodiethylene glycol (thiodiglycol, TDG) and methylthioethanol;
- the nonaqueous solvent is selected from sulfones, glycols and polyalkylene glycols. Most preferably, the nonaqueous solvent is selected from sulfones. A preferred nonaqueous solvent is sulfolane.
- the absorbent may also comprise additives such as corrosion inhibitors, enzymes, antifoams, etc.
- additives such as corrosion inhibitors, enzymes, antifoams, etc.
- the amount of such additives is in the range from about 0.005% to 3% by weight of the absorbent.
- the present invention also relates to the use of the absorbent and its embodiments as described above for removal of acid gases from a fluid stream, especially for selective removal of hydrogen sulfide from a fluid stream comprising carbon dioxide and hydrogen sulfide.
- mol ⁇ ( H 2 ⁇ S ) mol ⁇ ( CO 2 ) liquid phase is the molar H 2 S/CO 2 ratio in a liquid phase which is in contact with a gas phase and
- mol ⁇ ( H 2 ⁇ S ) mol ⁇ ( CO 2 ) gas phase is the molar H 2 S/CO 2 ratio in the gas phase.
- the liquid phase is the laden absorbent at the bottom of the absorber and the gas phase is the fluid stream to be treated.
- the process of the invention is suitable for treatment of all kinds of fluids.
- Fluids are firstly gases such as natural gas, synthesis gas, coke oven gas, cracking gas, coal gasification gas, cycle gas, landfill gases and combustion gases, and secondly liquids that are essentially immiscible with the absorbent, such as LPG (liquefied petroleum gas) or NGL (natural gas liquids).
- LPG liquefied petroleum gas
- NGL natural gas liquids
- the process of the invention is particularly suitable for treatment of hydrocarbonaceous fluid streams.
- the hydrocarbons present are, for example, aliphatic hydrocarbons such as C 1 -C 4 hydrocarbons such as methane, unsaturated hydrocarbons such as ethylene or propylene, or aromatic hydrocarbons such as benzene, toluene or xylene.
- the process of the invention is suitable for removal of acid gases, for example CO 2 , H 2 S, SO 3 , SO 2 , CS 2 , HCN, COS and mercaptans. It is also possible for other acidic gases to be present in the fluid stream, such as COS and mercaptans.
- acid gases for example CO 2 , H 2 S, SO 3 , SO 2 , CS 2 , HCN, COS and mercaptans.
- other acidic gases such as COS and mercaptans.
- the process is especially suitable for selective removal of hydrogen sulfide from a fluid stream comprising carbon dioxide and hydrogen sulphide and allows high H 2 S cleanup selectively at low solvent circulation rates.
- the process is useful in sulfur plant Tail Gas Treating Unit (TGTU) applications, in Acid-Gas Enrichment (AGE) processes to upgrade lean acid offgas from treating units to higher-quality Claus plant feed, or for the treatment of associated gases and refinery gases.
- TGTU sulfur plant Tail Gas Treating Unit
- AGE Acid-Gas Enrichment
- the fluid stream is contacted with the absorbent in an absorption step in an absorber, as a result of which carbon dioxide and hydrogen sulfide are at least partly scrubbed out.
- the absorber used is a scrubbing apparatus used in customary gas scrubbing processes.
- Suitable scrubbing apparatuses are, for example, random packings, columns having structured packings and having trays, membrane contactors, radial flow scrubbers, jet scrubbers, Venturi scrubbers and rotary spray scrubbers, preferably columns having structured packings, having random packings and having trays, more preferably columns having trays and having random packings.
- the fluid stream is preferably treated with the absorbent in a column in countercurrent. The fluid is generally fed into the lower region and the absorbent into the upper region of the column. Installed in tray columns are sieve trays, bubble-cap trays or valve trays, over which the liquid flows.
- Columns having random packings can be filled with different shaped bodies. Heat and mass transfer are improved by the increase in the surface area caused by the shaped bodies, which are usually about 25 to 80 mm in size.
- Known examples are the Raschig ring (a hollow cylinder), Pall ring, Hiflow ring, Intalox saddle and the like.
- the random packings can be introduced into the column in an ordered manner, or else randomly (as a bed). Possible materials include glass, ceramic, metal and plastics.
- Structured packings are a further development of ordered random packings. They have a regular structure. As a result, it is possible in the case of packings to reduce pressure drops in the gas flow. There are various designs of structured packings, for example woven packings or sheet metal packings. Materials used may be metal, plastic, glass and ceramic.
- the temperature of the absorbent in the absorption step is generally about 30 to 100° C., and when a column is used is, for example, 30 to 70° C. at the top of the column and 50 to 100° C. at the bottom of the column.
- the process of the invention may comprise one or more, especially two, successive absorption steps.
- the absorption can be conducted in a plurality of successive component steps, in which case the crude gas comprising the acidic gas constituents is contacted with a substream of the absorbent in each of the component steps.
- the absorbent with which the crude gas is contacted may already be partly laden with acidic gases, meaning that it may, for example, be an absorbent which has been recycled from a downstream absorption step into the first absorption step, or be partly regenerated absorbent.
- the person skilled in the art can achieve a high level of hydrogen sulfide removal with a defined selectivity by varying the conditions in the absorption step, such as, more particularly, the absorbent/fluid stream ratio, the column height of the absorber, the type of contact-promoting internals in the absorber, such as random packings, trays or structured packings, and/or the residual loading of the regenerated absorbent.
- the conditions in the absorption step such as, more particularly, the absorbent/fluid stream ratio, the column height of the absorber, the type of contact-promoting internals in the absorber, such as random packings, trays or structured packings, and/or the residual loading of the regenerated absorbent.
- the process preferably comprises a regeneration step in which the CO 2 - and H 2 S-laden absorbent is regenerated.
- the regeneration step CO 2 and H 2 S and optionally further acidic gas constituents are released from the CO 2 - and H 2 S-laden absorbent to obtain a regenerated absorbent.
- the regenerated absorbent is subsequently recycled into the absorption step.
- the regeneration step comprises at least one of the measures of heating, decompressing and stripping with an inert fluid.
- the regeneration step preferably comprises heating of the absorbent laden with the acidic gas constituents, for example by means of a boiler, natural circulation evaporator, forced circulation evaporator or forced circulation flash evaporator.
- the absorbed acid gases are stripped out by means of the steam obtained by heating the solution. Rather than steam, it is also possible to use an inert fluid such as nitrogen.
- the absolute pressure in the desorber is normally 0.1 to 3.5 bar, preferably 1.0 to 2.5 bar.
- the temperature is normally 50° C. to 170° C., preferably 80° C. to 130° C., the temperature of course being dependent on the pressure.
- the regeneration step may alternatively or additionally comprise a decompression.
- This includes at least one decompression of the laden absorbent from a high pressure as exists in the conduction of the absorption step to a lower pressure.
- the decompression can be accomplished, for example, by means of a throttle valve and/or a decompression turbine. Regeneration with a decompression stage is described, for example, in publications U.S. Pat. Nos. 4,537,753 and 4,553,984.
- the acidic gas constituents can be released in the regeneration step, for example, in a decompression column, for example a flash vessel installed vertically or horizontally, or a countercurrent column with internals.
- a decompression column for example a flash vessel installed vertically or horizontally, or a countercurrent column with internals.
- the regeneration column may likewise be a column having random packings, having structured packings or having trays.
- the regeneration column at the bottom, has a heater, for example a forced circulation evaporator with circulation pump. At the top, the regeneration column has an outlet for the acid gases released. Entrained absorption medium vapors are condensed in a condenser and recirculated to the column.
- regeneration can be effected in a preliminary decompression column at a high pressure typically about 1.5 bar above the partial pressure of the acidic gas constituents in the absorption step, and in a main decompression column at a low pressure, for example 1 to 2 bar absolute.
- Regeneration with two or more decompression stages is described in publications U.S. Pat. Nos. 4,537,753, 4,553,984, EP 0 159 495, EP 0 202 600, EP 0 190 434 and EP 0 121 109.
- FIG. 1 is a schematic diagram of a plant suitable for performing the process of the invention.
- FIG. 2 is a plot of the selectivity of H 2 S over CO 2 as a function of acid gas loading with different amine aqueous solutions an amine concentration of 36 wt.-%.
- FIG. 3 is a plot of the CO 2 and H 2 S uptake as a function of treatment time by aqueous amine solutions.
- FIG. 4 is a plot of the selectivity of H 2 S over CO 2 as a function of acid gas loading with different amine aqueous solutions an amine concentration of 2.17 M.
- FIG. 5 is a plot of the CO 2 and H 2 S uptake as a function of treatment time by aqueous amine solutions.
- a suitably pre-treated gas comprising hydrogen sulfide and carbon dioxide is contacted in counter-current, in an absorber A 1 , with regenerated absorbent which is fed in via the absorbent line 1 . 01 .
- the absorbent removes hydrogen sulfide and carbon dioxide from the gas by absorption; this affords a hydrogen sulfide- and carbon dioxide-depleted clean gas via the offgas line 1 . 02 .
- the heat exchanger 1 . 04 in which the CO 2 - and H 2 S-laden absorbent is heated up with the heat from the regenerated absorbent conducted through the absorbent line 1 . 05 , and the absorbent line 1 . 06 , the CO 2 - and H 2 S-laden absorbent is fed to the desorption column D and regenerated.
- one or more flash vessels may be provided (not shown in FIG. 1 ), in which the CO 2 - and H 2 S-laden absorbent is decompressed to, for example, 3 to 15 bar.
- the absorbent is conducted into the boiler 1 . 07 , where it is heated.
- the steam that arises is recycled into the desorption column D, while the regenerated absorbent is fed back to the absorber A 1 via the absorbent line 1 . 05 , the heat exchanger 1 . 04 in which the regenerated absorbent heats up the CO 2 - and H 2 S-laden absorbent and at the same time cools down itself, the absorbent line 1 . 08 , the cooler 1 . 09 and the absorbent line 1 . 01 .
- a mixed-phase stream of regenerated absorbent and steam is returned to the bottom of the desorption column D, where the phase separation between the vapor and the absorbent takes place.
- the regenerated absorbent to the heat exchanger 1 . 04 is either drawn off from the circulation stream from the bottom of the desorption column D to the evaporator or conducted via a separate line directly from the bottom of the desorption column D to the heat exchanger 1 . 04 .
- the CO 2 - and H 2 S-containing gas released in the desorption column D leaves the desorption column D via the offgas line 1 . 10 . It is conducted into a condenser with integrated phase separation 1 . 11 , where it is separated from entrained absorbent vapor. In this and all the other plants suitable for performance of the process of the invention, condensation and phase separation may also be present separately from one another. Subsequently, the condensate is conducted through the absorbent line 1 . 12 into the upper region of the desorption column D, and a CO 2 - and H 2 S-containing gas is discharged via the gas line 1 . 13 .
- a mixture of morpholine and 2-(2-tert-butylaminoethoxy)ethanol (molar ratio 2:1) was passed over the catalyst at 170 to 195° C. and a pressure of 70 bar together with hydrogen (10 NL/h).
- the 2-(2-tert-butylaminoethoxy)ethanol weight hourly space velocity was set to 0.2 kg/(l ⁇ h).
- the reaction output was analyzed by means of gas chromatography (column: 30 m Rtx-5 Amine from Restek, internal diameter: 0.32 mm, d f : 1.5 ⁇ m, temperature program 60° C. to 280° C. in steps of 4° C./min). The following analysis values are reported in GC area percent.
- the GC analysis showed a conversion of 73-98% based on 2-(2-tert-butylaminoethoxy)ethanol used, and tert-butylaminoethoxyethylmorpholine (TBAEEM) was obtained in a selectivity of 17-21%.
- the crude product was purified by distillation. After the removal of excess morpholine at 80° C. and 1 mbar, the target product was isolated at a distillation temperature of 64° C. at 1 mbar in a purity of >97%.
- An oil-heated glass reactor having a length of 0.9 m and an internal diameter of 28 mm was charged with 250 mL of V2A mesh rings (diameter 5 mm), above that 200 mL of a copper catalyst (support: alumina) and finally 550 mL of V2A mesh rings (diameter 5 mm).
- the catalyst was activated as follows: Over a period of 2 h, at 160° C., a gas mixture consisting of H 2 (5% by volume) and N 2 (95% by volume) was passed over the catalyst at 100 L/h. Thereafter, the catalyst was kept at a temperature of 180° C. for a further 2 h. Subsequently, at 200° C. over a period of 1 h, a gas mixture consisting of H 2 (10% by volume) and N 2 (90% by volume) was passed over the catalyst, then, at 200° C. over a period of 30 min, a gas mixture consisting of H 2 (30% by volume) and N 2 (70% by volume) and finally, at 200° C. over a period of 1 h, H 2 .
- the oil bath temperature was set to 180 to 200° C. 65-130 g/h of a mixture of tert-butylamine (TBA) and N-(2-hydroxyethyl)-morpholine (molar ratio of 4:1) was passed over the catalyst at 200° C. together with hydrogen (80 L/h).
- the reaction output was condensed by means of a jacketed coil condenser and analyzed by means of gas chromatography (column: 30 m DB1 from Agilent, internal diameter: 0.25 mm, d f : 1.0 ⁇ m, temperature program 80° C. to 280° C. in steps of 10° C./min). The following analysis values are reported in GC area percent.
- the GC analysis showed a conversion of 80% based on N-(2-hydroxyethyl)-morpholine used, and 2-methyl-N-(2-morpholinoethyl)-propane-2-amine was obtained in a selectivity of 90%.
- the crude product was purified by distillation. After the removal of excess tert-butylamine under standard pressure, the target product was isolated at a bottom temperature of 115° C. and a distillation temperature of 104° C. at 10 mbar in a purity of >99.7%.
- the process absorption unit is a semi-batch system, comprising a water saturator, a stirred autoclave to which gas can be fed in up-flow mode, and a condenser.
- the autoclave is equipped with a pressure gauge and a type J thermocouple.
- a safety rupture disc is attached to the autoclave head.
- a high wattage ceramic fiber heater is used to supply heat to the autoclave.
- the gas flows are regulated by Brooks mass flow controllers and the temperature of the condenser is maintained by a chiller.
- a custom LabVIEW program is used to control the PAU operation and to acquire experimental data (temperature, pressure, stirrer speed, pH, gas flow rate, and off-gas concentration).
- the experiments described hereinbelow were performed by flowing the test acid gas mixture through the autoclave in which the amine solution was previously loaded.
- the acid gas mixture was fed to the bottom of the reactor by-passing the water saturator.
- the gases leaving the autoclave were transferred through the condenser (maintained at 10° C.) in order to remove any entrained liquids.
- a slip-stream of the off-gas leaving the condenser was piped to a micron-GC (Inficon) for analysis while the main gas flow passed through a scrubber. After reaching breakthrough, nitrogen was used to purge the system.
- the off-gas composition was measured using a custom-built micro GC.
- the micro GC is configured as a refinery Gas Analyzer and includes four columns (Mole Sieve, PLOT U, OV-1, PLOT Q) and four TCD detectors.
- a slip stream of the off-gas was injected into the micro GC approximately every 2 minutes.
- a small internal vacuum pump was used to transfer the sample into the micro GC.
- the nominal pump rate was ⁇ 20 mL/min in order to achieve 10 ⁇ the volume of line flushes between the sample tee and the micro GC.
- the actual gas injected into the micro GC was ⁇ 1 ⁇ L.
- the PLOT U column was used to separate and identify H 2 S and CO 2
- the micro TCD was used to quantify H 2 S and CO 2 .
- Example 1 amine aqueous solutions at a concentration of 36 wt.-% amine were tested.
- Test conditions for Example 1 were as follows: gas feed composition: 10 mol % CO 2 , 1 mol % H 2 S, balance N 2 ; gas flow rate: 154 sccm; temperature: 40.8° C., pressure: 1 bar; volume: 15 mL; stirring rate: 200 rpm.
- FIG. 2 is a plot of the selectivity of H 2 S over CO 2 as a function of acid gas loading with different amine aqueous solutions.
- FIG. 3 is a plot of the CO 2 and H 2 S uptake as a function of treatment time by aqueous amine solutions.
- Example 2 amine aqueous solutions at a molar concentration of 2.17 M amine were tested.
- Test conditions for Example 2 were as follows: gas feed composition: 10 mol % CO 2 , 1 mol % H 2 S, balance N 2 ; gas flow rate: 154 sccm; temperature: 40.8° C., pressure: 1 bar; volume: 15 mL; stirring rate: 200 rpm.
- FIG. 4 is a plot of the selectivity of H 2 S over CO 2 as a function of acid gas loading with different amine aqueous solutions.
- FIG. 5 is a plot of the CO 2 and H 2 S uptake as a function of treatment time by aqueous amine solutions.
- the volatility of M3ETB, TBAEEM and TBAEE was measured for 30 wt.-% aqueous solutions.
- a glass condenser which was operated at 5° C., was attached to a glass cylinder with a thermostated jacket. The glass cylinder was thermostated to 50° C., and 200 mL of the absorbent were introduced in each case. Over an experimental duration of 8 h, 30 NL/h of N 2 were passed through the absorbent at ambient pressure. Thereafter, the condensate obtained in the glass condenser was separated and analyzed for its composition by GC analysis and Karl-Fischer titration.
- Solutions having a collapse smaller than 30 sec can be considered as solutions having a low foaming tendency. Solutions with collapse time >30 sec have a strong foaming tendency. It can be seen that TBAEEM and TBAEM have a significant smaller foaming tendency compared to the reference example.
- Sour loading capacities of M3ETB, TBAEEM, TBAEM, TBAEE, MDEA, and Bis-MOE were measured for 30 wt.-% aqueous solutions.
- a glass condenser which was operated at 5° C., was attached to a glass cylinder with a thermostated jacket. This prevented distortion of the test results by partial evaporation of the absorbent.
- the glass cylinder was initially charged with about 100 mL of unladen absorbent (30% by weight of amine in water). To determine the absorption capacity, at ambient pressure and 40° C., 8 NL/h of CO 2 or H 2 S were passed through the absorption liquid via a frit over a period of about 4 h. Subsequently, the loading of CO 2 or H 2 S was determined as follows:
- H 2 S The determination of H 2 S was effected by titration with silver nitrate solution.
- the sample to be analyzed was weighed into an aqueous solution together with about 2% by weight of sodium acetate and about 3% by weight of ammonia.
- the H 2 S content was determined by a potentiometric turning point titration by means of silver nitrate. At the turning point, the H 2 S is fully bound as Ag 2 S.
- the CO 2 content was determined as total inorganic carbon (TOC-V Series Shimadzu).
- the laden solution was stripped by heating an identical apparatus setup to 80° C., introducing the laden absorbent and stripping it by means of an N 2 stream (8 NL/h). After 60 min, a sample was taken and the CO 2 or H 2 S loading of the absorbent was determined as described above.
- TBAEEM has a higher cyclic capacity for CO 2 compared to the reference amines MDEA, TBAEE, TBAEM, M3ETB and Bis-MOE. Further, it can be seen that TBAEEM has a higher cyclic capacity for H 2 S compared to Bis-MOE.
Abstract
Description
R1 through R4 are selected from H and alkyl, whereas R5 and R6 are alkyl or R5 and R6 together form a cycle. These compounds, incorporating only tertiary amino groups, are expected to exhibit limited H2S capacity since H2S capacity attributed to tertiary amino groups is known to be lower than that of, e.g., sterically hindered secondary amino groups.
in which R1 and R2 are independently C1-C4-alkyl; R3 is selected from hydrogen and C1-C4-alkyl, R4, R5 and R6 are independently selected from hydrogen and C1-C4-alkyl; x and y are integers from 2 to 4 and z is an integer from 1 to 3.
R9—PO3H (II)
in which R10 is H or C1-6-alkyl, Q is H, OH or NY2 and Y is H or CH2PO3H2, such as 1-hydroxyethane-1,1-diphosphonic acid;
in which Z is C2-6-alkylene, cycloalkanediyl, phenylene, or C2-6-alkylene interrupted by cycloalkanediyl or phenylene, Y is CH2PO3H2 and m is 0 to 4, such as ethylenediaminetetra(methylenephosphonic acid), diethylenetriamine-penta(methylenephosphonic acid) and bis(hexamethylene)triaminepenta-(methylenephosphonic acid);
R11—NY2 (V)
where
liquid phase is the molar H2S/CO2 ratio in a liquid phase which is in contact with a gas phase and
gas phase is the molar H2S/CO2 ratio in the gas phase. In a standard gas scrubbing process, the liquid phase is the laden absorbent at the bottom of the absorber and the gas phase is the fluid stream to be treated.
- MDEA: methyldiethanolamine
- TBAEE: tert-butylamine ethoxyethanol
- M3ETB: methoxyethoxyethoxyethyl-tert-butylamine
- TBAEEM: tert-butylaminoethoxyethylmorpholine
- TBAEM: tert-butylaminoethylmorpholine
- Bis-MOE: bis-(2-morpholinoethyl)ether
Amount of condensate | Water | Amine | |
Solution | [g] | [g/100 g] | [g/100 g] |
30% M3ETB* | 30.1 | 99.2 | 0.7 |
30% TBAEE* | 30 | 99.3 | 0.7 |
30% MDEA* | 27.1 | 99.4 | 0.7 |
30% TBAEEM | 30.5 | 99.6 | 0.2 |
*comparative example |
TBAEE | TBAEEM | TBAEM | |||
collapse time [sec] | 32 | 23 | 23 | ||
CO2 loading | CO2 loading | Cyclic | ||
after loading | after stripping | Capacity | ||
(molCO2/ | (molCO2/ | (molCO2/ | ||
Run | Absorbent | molamine) | molamine) | molamine) |
1 | 30 wt.-% MDEA | 0.77 | 0.05 | 0.72 |
2 | 30 wt.-% TBAEE | 0.97 | 0.24 | 0.73 |
3 | 30 wt.-% M3ETB | 0.97 | 0.17 | 0.80 |
4 | 30 wt.-% TBAEEM | 1.04 | 0.01 | 1.03 |
5 | 30 wt.-% TBAEM | 0.93 | 0.03 | 0.90 |
6 | 30 wt.-% Bis-MOE | 0.25 | 0.02 | 0.23 |
H2S loading | H2S loading | |||
after | after | Cyclic | ||
loading | stripping | Capacity | ||
(molH2S/ | (molH2S/ | (molH2S/ | ||
Run | Absorbent | molamine) | molamine) | molamine) |
7 | 30 wt.-% TBAEEM | 1.04 | 0.03 | 1.01 |
8 | 30 wt.-% Bis-MOE | 0.26 | 0.01 | 0.25 |
Claims (11)
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP16166787.8 | 2016-04-25 | ||
EP16166787 | 2016-04-25 | ||
EP16166787 | 2016-04-25 | ||
PCT/EP2017/058122 WO2017186466A1 (en) | 2016-04-25 | 2017-04-05 | Use of morpholine-based hindered amine compounds for selective removal of hydrogen sulfide |
Publications (2)
Publication Number | Publication Date |
---|---|
US20190143262A1 US20190143262A1 (en) | 2019-05-16 |
US10525404B2 true US10525404B2 (en) | 2020-01-07 |
Family
ID=55809007
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US16/095,970 Active US10525404B2 (en) | 2016-04-25 | 2017-04-05 | Use of morpholine-based hindered amine compounds for selective removal of hydrogen sulfide |
Country Status (10)
Country | Link |
---|---|
US (1) | US10525404B2 (en) |
EP (1) | EP3448543B1 (en) |
JP (1) | JP6945617B2 (en) |
CN (1) | CN109069984B (en) |
BR (1) | BR112018071876B1 (en) |
CA (1) | CA3021567C (en) |
EA (1) | EA036128B1 (en) |
ES (1) | ES2817475T3 (en) |
SA (1) | SA518400312B1 (en) |
WO (1) | WO2017186466A1 (en) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20190126193A1 (en) * | 2016-04-18 | 2019-05-02 | Basf Se | Premix for producing an absorption agent for removing acid gases from a fluid flow |
US11241652B2 (en) | 2017-05-15 | 2022-02-08 | Basf Se (Reitstötter, Kinzebach & Partner) | Absorbent and process for selectively removing hydrogen sulfide |
WO2022129977A1 (en) | 2020-12-17 | 2022-06-23 | Totalenergies Onetech | Method for recovering high purity carbon dioxide from a gas mixture |
WO2022129975A1 (en) | 2020-12-17 | 2022-06-23 | Totalenergies Onetech | Method for the selective removal of hydrogen sulfide from a gas stream |
WO2022129974A1 (en) | 2020-12-17 | 2022-06-23 | Totalenergies Onetech | Method for the selective removal of hydrogen sulfide from a gas stream |
WO2024059201A1 (en) | 2022-09-16 | 2024-03-21 | Saudi Arabian Oil Company | Hydrogen production by sulfur steam reforming |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2018146233A1 (en) | 2017-02-10 | 2018-08-16 | Basf Se | Process for removal of acid gases from a fluid stream |
BR112020003944A2 (en) * | 2017-09-04 | 2020-12-01 | Basf Se | absorbent and selective removal process |
EA202192258A1 (en) * | 2019-02-18 | 2021-11-15 | Басф Се | METHOD FOR REMOVING ACID GASES FROM A FLUID STREAM USING LIQUID ABSORBENT CONTAINING PIPERAZINE RING |
BR112021023742A2 (en) | 2019-09-10 | 2022-04-12 | Basf Se | Process for removing acid gases from a fluid stream, use of an absorbent, and process for manufacturing a compound of formula (i) |
CN111905804A (en) * | 2020-08-12 | 2020-11-10 | 韩兆保 | HZB salt-inhibiting desulfurizing agent |
Citations (21)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0121109A2 (en) | 1983-03-08 | 1984-10-10 | BASF Aktiengesellschaft | Process for the removal of CO2 and/or H2S from gases |
EP0124835A2 (en) | 1983-05-04 | 1984-11-14 | Air Products And Chemicals, Inc. | BIS tertiary amino alkyl derivatives as solvents for acid gas removal from gas streams |
US4537753A (en) | 1982-10-02 | 1985-08-27 | Basf Aktiengesellschaft | Removal of CO2 and H2 S from natural gases |
EP0159495A2 (en) | 1984-03-10 | 1985-10-30 | BASF Aktiengesellschaft | Process for the removal of CO2 and/or H2S from gases |
US4553984A (en) | 1984-03-06 | 1985-11-19 | Basf Aktiengesellschaft | Removal of CO2 and/or H2 S from gases |
EP0190434A2 (en) | 1984-12-11 | 1986-08-13 | BASF Aktiengesellschaft | Process for removing CO2 and/or H2S from gases |
EP0359991A1 (en) | 1988-08-19 | 1990-03-28 | BASF Aktiengesellschaft | Process for removing carbon dioxide and possibly hydrogen sulphide from gases |
CA1295810C (en) | 1985-05-22 | 1992-02-18 | Eckhart Wagner | Removal of co- and/or h-s from gases |
WO2001000271A1 (en) | 1999-03-23 | 2001-01-04 | Acculaser, Inc. | Low level laser therapy apparatus |
WO2011067199A1 (en) | 2009-12-03 | 2011-06-09 | Basf Se | Catalyst and method for producing an amine |
US20130011314A1 (en) | 2009-12-16 | 2013-01-10 | Fabien Porcheron | Method of removing acid compounds from a gaseous effluent with an absorbent solution based on i, ii/iii diamines |
WO2014001664A1 (en) | 2012-06-26 | 2014-01-03 | IFP Energies Nouvelles | Absorbent solution made from tertiary diamines belonging to the hindered aminoethyl morpholine family and method for eliminating acid compounds from a gaseous effluent |
US20150027055A1 (en) | 2013-07-29 | 2015-01-29 | Exxonmobil Research And Engineering Company | Separation of hydrogen sulfide from natural gas |
US20170282116A1 (en) | 2014-08-25 | 2017-10-05 | Basf Se | Removal of carbon dioxide from a fluid flow |
US20180186725A1 (en) | 2015-05-28 | 2018-07-05 | Basf Se | Method for the homogeneous catalytic reductive amination of carbonyl compounds |
US20180221811A1 (en) | 2014-08-25 | 2018-08-09 | Basf Se | Absorbent for selective removal of hydrogen sulfide from a fluid stream |
US20180272271A1 (en) | 2015-09-29 | 2018-09-27 | Basf Se | Cyclic amine for selectively removing hydrogen sulphide |
US20180297926A1 (en) | 2015-10-12 | 2018-10-18 | Basf Se | Hydroformylation process for producing 1,6-disubstituted hexane derivatives |
US20180311611A1 (en) | 2015-09-29 | 2018-11-01 | Basf Se | Absorbent for the selective removal of hydrogen sulfide |
US10207217B2 (en) | 2014-08-25 | 2019-02-19 | Basf Se | Removal of hydrogen sulphide and carbon dioxide from a stream of fluid |
US10214482B2 (en) | 2014-08-25 | 2019-02-26 | Basf Se | Diamine having tert-alkylamino group and primary amino group for use in gas scrubbing |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
BR112014019344B1 (en) * | 2012-02-08 | 2021-04-27 | Nippon Steel Corporation | AQUEOUS SOLUTION THAT EFFICIENTLY ABSORVES CARBON DIOXIDE IN EXHAUST GAS AND METHOD TO RECOVER CARBON DIOXIDE USING THE SAME |
WO2014004019A1 (en) * | 2012-06-29 | 2014-01-03 | Dow Global Technologies Llc | Aqueous alkanolamine absorbent composition comprising piperazine for enhanced removal of hydrogen sulfide from gaseous mixtures and method for using the same |
CN103920380A (en) * | 2013-01-15 | 2014-07-16 | 永清华茂生物药业有限公司 | Desulfurizing agent |
CN105126576A (en) * | 2015-07-29 | 2015-12-09 | 中国石油集团工程设计有限责任公司 | High-efficiency composite desulphurization solvent and system and method for removing acidic gas and organic sulfur |
CN105413396A (en) * | 2015-10-21 | 2016-03-23 | 中石化节能环保工程科技有限公司 | Layered absorbent for trapping CO2 in tail gas |
-
2017
- 2017-04-05 US US16/095,970 patent/US10525404B2/en active Active
- 2017-04-05 WO PCT/EP2017/058122 patent/WO2017186466A1/en active Application Filing
- 2017-04-05 ES ES17714493T patent/ES2817475T3/en active Active
- 2017-04-05 JP JP2019506779A patent/JP6945617B2/en active Active
- 2017-04-05 BR BR112018071876-9A patent/BR112018071876B1/en active IP Right Grant
- 2017-04-05 CA CA3021567A patent/CA3021567C/en active Active
- 2017-04-05 CN CN201780025386.3A patent/CN109069984B/en active Active
- 2017-04-05 EP EP17714493.8A patent/EP3448543B1/en active Active
- 2017-04-05 EA EA201892387A patent/EA036128B1/en not_active IP Right Cessation
-
2018
- 2018-10-25 SA SA518400312A patent/SA518400312B1/en unknown
Patent Citations (26)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4537753A (en) | 1982-10-02 | 1985-08-27 | Basf Aktiengesellschaft | Removal of CO2 and H2 S from natural gases |
EP0121109A2 (en) | 1983-03-08 | 1984-10-10 | BASF Aktiengesellschaft | Process for the removal of CO2 and/or H2S from gases |
US4551158A (en) | 1983-03-08 | 1985-11-05 | Basf Aktiengesellschaft | Removal of CO2 and/or H2 S from gases |
EP0124835A2 (en) | 1983-05-04 | 1984-11-14 | Air Products And Chemicals, Inc. | BIS tertiary amino alkyl derivatives as solvents for acid gas removal from gas streams |
US4553984A (en) | 1984-03-06 | 1985-11-19 | Basf Aktiengesellschaft | Removal of CO2 and/or H2 S from gases |
EP0159495A2 (en) | 1984-03-10 | 1985-10-30 | BASF Aktiengesellschaft | Process for the removal of CO2 and/or H2S from gases |
US4997630A (en) | 1984-03-10 | 1991-03-05 | Basf Aktiengesellschaft | Removal of CO2 and/or H2 S from gases |
EP0190434A2 (en) | 1984-12-11 | 1986-08-13 | BASF Aktiengesellschaft | Process for removing CO2 and/or H2S from gases |
CA1290553C (en) | 1984-12-11 | 1991-10-15 | Eckhart Wagner | Removal of co -and/or h s from gases |
CA1295810C (en) | 1985-05-22 | 1992-02-18 | Eckhart Wagner | Removal of co- and/or h-s from gases |
EP0359991A1 (en) | 1988-08-19 | 1990-03-28 | BASF Aktiengesellschaft | Process for removing carbon dioxide and possibly hydrogen sulphide from gases |
US4999031A (en) | 1988-08-19 | 1991-03-12 | Basf Aktiengesellschaft | Removing CO2 and, if necessary, H2 S from gases |
WO2001000271A1 (en) | 1999-03-23 | 2001-01-04 | Acculaser, Inc. | Low level laser therapy apparatus |
US8487135B2 (en) | 2009-12-03 | 2013-07-16 | Basf Se | Catalyst and process for preparing an amine |
WO2011067199A1 (en) | 2009-12-03 | 2011-06-09 | Basf Se | Catalyst and method for producing an amine |
US20130011314A1 (en) | 2009-12-16 | 2013-01-10 | Fabien Porcheron | Method of removing acid compounds from a gaseous effluent with an absorbent solution based on i, ii/iii diamines |
WO2014001664A1 (en) | 2012-06-26 | 2014-01-03 | IFP Energies Nouvelles | Absorbent solution made from tertiary diamines belonging to the hindered aminoethyl morpholine family and method for eliminating acid compounds from a gaseous effluent |
US20150027055A1 (en) | 2013-07-29 | 2015-01-29 | Exxonmobil Research And Engineering Company | Separation of hydrogen sulfide from natural gas |
US10207217B2 (en) | 2014-08-25 | 2019-02-19 | Basf Se | Removal of hydrogen sulphide and carbon dioxide from a stream of fluid |
US20170282116A1 (en) | 2014-08-25 | 2017-10-05 | Basf Se | Removal of carbon dioxide from a fluid flow |
US20180221811A1 (en) | 2014-08-25 | 2018-08-09 | Basf Se | Absorbent for selective removal of hydrogen sulfide from a fluid stream |
US10214482B2 (en) | 2014-08-25 | 2019-02-26 | Basf Se | Diamine having tert-alkylamino group and primary amino group for use in gas scrubbing |
US20180186725A1 (en) | 2015-05-28 | 2018-07-05 | Basf Se | Method for the homogeneous catalytic reductive amination of carbonyl compounds |
US20180311611A1 (en) | 2015-09-29 | 2018-11-01 | Basf Se | Absorbent for the selective removal of hydrogen sulfide |
US20180272271A1 (en) | 2015-09-29 | 2018-09-27 | Basf Se | Cyclic amine for selectively removing hydrogen sulphide |
US20180297926A1 (en) | 2015-10-12 | 2018-10-18 | Basf Se | Hydroformylation process for producing 1,6-disubstituted hexane derivatives |
Non-Patent Citations (6)
Title |
---|
International Search Report for PCT/EP2017/058122 dated May 11, 2017. |
U.S. Appl. No. 15/781,555, filed Jun. 1, 2018. |
U.S. Appl. No. 16/074,100, filed Jul. 31, 2018. |
U.S. Appl. No. 16/093,731, filed Oct. 15, 2018. |
U.S. Appl. No. 16/238,069, filed Jan. 2, 2019. |
Written Opinion of the International Searching Authority for PCT/EP2017/058122 dated May 11, 2017. |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20190126193A1 (en) * | 2016-04-18 | 2019-05-02 | Basf Se | Premix for producing an absorption agent for removing acid gases from a fluid flow |
US11045759B2 (en) * | 2016-04-18 | 2021-06-29 | Basf Se | Premix for producing an absorption agent for removing acid gases from a fluid flow |
US11241652B2 (en) | 2017-05-15 | 2022-02-08 | Basf Se (Reitstötter, Kinzebach & Partner) | Absorbent and process for selectively removing hydrogen sulfide |
WO2022129977A1 (en) | 2020-12-17 | 2022-06-23 | Totalenergies Onetech | Method for recovering high purity carbon dioxide from a gas mixture |
WO2022129975A1 (en) | 2020-12-17 | 2022-06-23 | Totalenergies Onetech | Method for the selective removal of hydrogen sulfide from a gas stream |
WO2022129974A1 (en) | 2020-12-17 | 2022-06-23 | Totalenergies Onetech | Method for the selective removal of hydrogen sulfide from a gas stream |
WO2024059201A1 (en) | 2022-09-16 | 2024-03-21 | Saudi Arabian Oil Company | Hydrogen production by sulfur steam reforming |
Also Published As
Publication number | Publication date |
---|---|
JP6945617B2 (en) | 2021-10-06 |
BR112018071876B1 (en) | 2023-04-25 |
EA036128B1 (en) | 2020-10-01 |
CN109069984B (en) | 2021-09-03 |
EA201892387A1 (en) | 2019-03-29 |
EP3448543A1 (en) | 2019-03-06 |
WO2017186466A1 (en) | 2017-11-02 |
CA3021567C (en) | 2024-01-23 |
US20190143262A1 (en) | 2019-05-16 |
CA3021567A1 (en) | 2017-11-02 |
SA518400312B1 (en) | 2021-07-14 |
EP3448543B1 (en) | 2020-06-10 |
JP2019514684A (en) | 2019-06-06 |
BR112018071876A2 (en) | 2019-02-19 |
CN109069984A (en) | 2018-12-21 |
ES2817475T3 (en) | 2021-04-07 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US10525404B2 (en) | Use of morpholine-based hindered amine compounds for selective removal of hydrogen sulfide | |
US11130094B2 (en) | Cyclic amine for selectively removing hydrogen sulphide | |
US11173446B2 (en) | Process for removal of acid gases from a fluid stream | |
US11241652B2 (en) | Absorbent and process for selectively removing hydrogen sulfide | |
US20180272270A1 (en) | Amine compounds for selectively removing hydrogen sulphide | |
US11458433B2 (en) | Absorbent and process for selectively removing hydrogen sulfide | |
JP2018531242A6 (en) | Amine compounds for selective removal of hydrogen sulfide | |
US20220152551A1 (en) | Process for removal of acid gases from a fluid stream with a liquid absorbent comprising a piperazine ring |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
FEPP | Fee payment procedure |
Free format text: ENTITY STATUS SET TO UNDISCOUNTED (ORIGINAL EVENT CODE: BIG.); ENTITY STATUS OF PATENT OWNER: LARGE ENTITY |
|
AS | Assignment |
Owner name: EXXONMOBIL RESEARCH AND ENGINEERING COMPANY, VIRGI Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:PEREIRA, CARLA;SISKIN, MICHAEL;INGRAM, THOMAS;AND OTHERS;SIGNING DATES FROM 20180427 TO 20181029;REEL/FRAME:048275/0305 Owner name: BASF SE, GERMANY Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:PEREIRA, CARLA;SISKIN, MICHAEL;INGRAM, THOMAS;AND OTHERS;SIGNING DATES FROM 20180427 TO 20181029;REEL/FRAME:048275/0305 |
|
STPP | Information on status: patent application and granting procedure in general |
Free format text: NOTICE OF ALLOWANCE MAILED -- APPLICATION RECEIVED IN OFFICE OF PUBLICATIONS |
|
STPP | Information on status: patent application and granting procedure in general |
Free format text: PUBLICATIONS -- ISSUE FEE PAYMENT VERIFIED |
|
STCF | Information on status: patent grant |
Free format text: PATENTED CASE |
|
AS | Assignment |
Owner name: EXXONMOBIL TECHNOLOGY AND ENGINEERING COMPANY, NEW JERSEY Free format text: CHANGE OF NAME;ASSIGNOR:EXXONMOBIL RESEARCH AND ENGINEERING COMPANY;REEL/FRAME:062221/0078 Effective date: 20220401 |
|
MAFP | Maintenance fee payment |
Free format text: PAYMENT OF MAINTENANCE FEE, 4TH YEAR, LARGE ENTITY (ORIGINAL EVENT CODE: M1551); ENTITY STATUS OF PATENT OWNER: LARGE ENTITY Year of fee payment: 4 |